CN217535928U - Conversion condensate energy recovery system - Google Patents
Conversion condensate energy recovery system Download PDFInfo
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- CN217535928U CN217535928U CN202220456540.0U CN202220456540U CN217535928U CN 217535928 U CN217535928 U CN 217535928U CN 202220456540 U CN202220456540 U CN 202220456540U CN 217535928 U CN217535928 U CN 217535928U
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Abstract
The utility model relates to a coal chemical industry transform condensate treatment process technical field discloses a transform condensate energy recuperation system: the system comprises a first energy recovery module, a second energy recovery module, a third energy recovery module and a stripping tower; wherein the first energy recovery module is connected with the stripping tower, the second energy recovery module is connected with the third energy recovery module, and the third energy recovery module is connected with the stripping tower. The utility model provides a transform condensate energy recuperation system, but make full use of high temperature condensate and the temperature and the pressure of medium temperature condensate to and the pressure of low temperature condensate, reduce the quantity of the reboiling steam of low temperature condensate strip tower, improve the energy comprehensive utilization of whole technology.
Description
Technical Field
The utility model relates to a coal chemical industry transform condensate treatment process technical field, concretely relates to transform condensate energy recuperation system.
Background
The gasification of the coal water slurry is generally carried out under the conditions of 6.5MPa (G) and 1200-1350 ℃, and high-temperature and high-pressure crude synthesis gas containing components such as hydrogen, carbon monoxide, carbon dioxide and the like can be obtained. After gas-liquid separation, one part of the high-temperature high-pressure crude synthesis gas is subjected to heat exchange and washing, and then is sent to a conversion unit for CO conversion reaction to generate hydrogen and carbon dioxide; the other part is sent to a gas distribution line after heat exchange and washing to adjust the ratio of hydrogen to carbon monoxide, and different downstream products can be correspondingly produced.
The conversion condensate generated in the treatment process of the high-temperature and high-pressure raw synthesis gas from the gasification unit can be divided into three grades according to the heat requirement: high-temperature condensate at a temperature of generally 190-240 ℃, medium-temperature condensate at a temperature of generally 150-180 ℃ and low-temperature condensate at a temperature of generally 30-50 ℃. At present, in coal chemical production, high-temperature process condensate and medium-temperature process condensate are generally returned to a gasification unit to be used as washing water, and low-temperature process condensate is independently sent to a stripping tower to be subjected to deamination and denitrification treatment.
However, this treatment mainly has the following drawbacks: 1) The high-temperature process condensate and the medium-temperature process condensate are generally mixed in a condensing tank, so that heat loss is easily caused, and the heat utilization efficiency is reduced; 2) The high-temperature and medium-temperature condensate liquid returns to the gasification unit to be used as washing water, and deamination and denitrification treatment are avoided; 3) When the low-temperature condensate is subjected to deamination and denitrification treatment in the stripping tower, the steam consumption is large due to the low temperature of the low-temperature condensate.
Therefore, the conversion condensate energy recovery system with high energy comprehensive utilization rate and good deamination and denitrification effects is urgently needed to be provided.
SUMMERY OF THE UTILITY MODEL
The utility model aims at solving the coal chemical industry and changeing condensate calorific loss big, energy utilization is low, and the not good problem of deamination denitrogenation effect provides a transform condensate energy recuperation system, and this system has heat and pressure energy high-usage, and the effectual advantage of deamination denitrogenation is fit for the industrialization and promotes.
In order to achieve the above object, the present invention provides a conversion condensate energy recovery system, wherein the system comprises a first energy recovery module 1, a second energy recovery module 2, a third energy recovery module 3 and a stripping tower 4; wherein the first energy recovery module 1 is connected to the stripping column 4, the second energy recovery module 2 is connected to the third energy recovery module 3, and the third energy recovery module 3 is connected to the stripping column 4.
Preferably, the first energy recovery module 1 is selected from a differential steam pressure power plant and/or a pressure driven pump for recovering the pressure of the low temperature condensate to generate electrical energy and/or driving force.
Preferably, the second energy recovery module 2 is selected from a heat exchanger and/or a heat storage device for recovering heat from the high temperature condensate.
Preferably, the third energy recovery module 3 is selected from a differential steam pressure power generation device and/or a pressure driven pump for recovering the pressure of the medium temperature condensate and the high temperature condensate from the second energy recovery module 2 to generate electric energy and/or driving force.
Preferably, the system further comprises a stripping cooler 5, a circulating water cooler 6 and a gas-liquid separation tank 7; the stripping tower 4 is sequentially connected with the stripping cooler 5, the circulating water cooler 6 and the gas-liquid separation tank 7, and the gas-liquid separation tank 7 is also connected with the stripping cooler 5.
Preferably, the top of the separation tank is provided with a washing device 8, and the washing device 8 is used for washing the non-condensable gas from the gas-liquid separation tank 7 so as to remove trace ammonia carried in the non-condensable gas.
Preferably, the system further comprises a circulating pump 9, wherein the circulating pump 9 is arranged between the stripping cooler 5 and the gas-liquid separation tank 7, and is used for conveying the liquid phase separated in the gas-liquid separation tank 7 to the stripping cooler 5 to exchange heat with the stripping gas extracted from the top of the stripping tower 4.
Preferably, the system further comprises a high-pressure flash gas pipeline 10, wherein the high-pressure flash gas pipeline 10 is connected with the stripping tower 4 and is used for conveying high-pressure flash gas to the stripping tower 4.
Preferably, the system further comprises an auxiliary steam line 11, said auxiliary steam line 11 being connected to said stripping column 4 for regulating the amount of steam entering said stripping column 4.
Through the technical scheme, the utility model discloses the beneficial technological effect who gains as follows:
1) The utility model provides a transform condensate liquid energy recuperation system utilizes first energy recuperation module and third energy recuperation module to retrieve the pressure energy of low temperature condensate, high temperature condensate and medium temperature condensate to can be used for generating electricity or as drive power with the pressure energy of retrieving, improved the utilization ratio of pressure in low temperature condensate, high temperature condensate and the medium temperature condensate;
2) The utility model provides a pair of transform condensate liquid energy recuperation system, utilize second energy recuperation module to retrieve the heat of high temperature condensate, and introduce the strip tower of handling low temperature condensate with high temperature condensate and medium temperature condensate, not only can handle high temperature simultaneously, medium temperature and low temperature condensate, saving equipment, simplify process flow, can also make full use of the heat of high temperature and medium temperature condensate, reduce the steam consumption of strip tower, improve the effect of deamination denitrogenation, water purification, realize reducing the mesh of whole system ammonia nitrogen content, make the condensate after strip tower is handled can directly send gasification unit to use as the washing water;
3) The utility model provides a transform condensate energy recuperation system carries out two-stage cooling to the stripping gas of following the stripper top of the tower through setting up strip cooler and circulating water cooler to the liquid phase that will condense in the gas-liquid separation jar gets off returns strip cooler and is used for cooling the stripping gas of following the stripper top of the tower, can improve the separation efficiency of gas-liquid separation jar, further improves thermal comprehensive utilization ability;
4) The utility model provides a pair of transform condensate energy recuperation system utilizes high-pressure flash distillation vapour to strip, helps retrieving hydrogen and carbon monoxide in high-pressure flash distillation vapour and the high temperature condensate.
Drawings
Fig. 1 is a schematic structural diagram of an energy recovery system for transforming condensate provided by the present invention.
Description of the reference numerals
1, a first energy recovery module 2, a second energy recovery module 3 and a third energy recovery module
4 stripping tower 5, stripping cooler 6 and circulating water cooler
7, a gas-liquid separation tank 8, a washing device 9 and a circulating pump
10, high-pressure flash gas pipeline 11 and auxiliary steam pipeline
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For numerical ranges, each range between its endpoints and individual point values, and each individual point value can be combined with each other to give one or more new numerical ranges, and such numerical ranges should be construed as specifically disclosed herein.
The utility model provides a conversion condensate energy recovery system, wherein, the system comprises a first energy recovery module 1, a second energy recovery module 2, a third energy recovery module 3 and a stripping tower 4; wherein the first energy recovery module 1 is connected to the stripping tower 4, the second energy recovery module 2 is connected to the third energy recovery module 3, and the third energy recovery module 3 is connected to the stripping tower 4, as shown in fig. 1.
In a preferred embodiment, the first energy recovery module 1 is selected from a differential steam pressure power plant and/or a pressure driven pump for recovering the pressure of the low temperature condensate for generating electrical energy and/or driving force.
In a preferred embodiment, the second energy recovery module 2 is selected from a heat exchanger and/or a heat storage device for recovering heat from the high-temperature condensate. For example, deoxygenated water, 0.4MPa low pressure steam, or other process media may be heated.
In a preferred embodiment, the third energy recovery module 3 is selected from a differential steam pressure power plant and/or a pressure driven pump for recovering the pressure of the medium temperature condensate and the high temperature condensate from the second energy recovery module 2 to generate electrical energy and/or driving force.
Wherein, the inventor of the utility model discovers through the research, utilizes the second energy recovery module to retrieve the heat of high temperature condensate, utilizes first energy recovery module and third energy recovery module to retrieve low temperature condensate, high temperature condensate and the pressure of medium temperature condensate to introduce the stripper of handling low temperature condensate with high temperature condensate and medium temperature condensate, can reduce the steam consumption of stripper, improve the energy comprehensive utilization of whole technology.
In a preferred embodiment, the stripping column 4 is a tray column, wherein the first energy module 1 is connected to the top of the stripping column 4 for feeding low-temperature condensate to the first tray of the stripping column.
In a preferred embodiment, the system further comprises a stripping cooler 5, a circulating water cooler 6, and a gas-liquid separation tank 7; the stripping tower 4 is sequentially connected with the stripping cooler 5, the circulating water cooler 6 and the gas-liquid separation tank 7, and the gas-liquid separation tank 7 is also connected with the stripping cooler 5.
Wherein, the utility model discloses in, the stripping gas of following the extraction tower top of the tower gets into the gas-liquid separation jar after stripping cooler and circulating water cooler two-stage cooling, and the liquid phase that gets off in the gas-liquid separation jar condenses back to the stripping cooler and is used for cooling the stripping gas of following the extraction tower top of the tower, can improve the separation efficiency of gas-liquid separation jar, further improves the comprehensive utilization of energy. And the liquid phase after heat exchange enters a carbon dioxide removal module to obtain dilute ammonia water which can be used as ammonia water or a liquid ammonia production raw material.
In a preferred embodiment, the top of the separation tank is provided with a washing device 8, and the washing device 8 is used for washing the non-condensable gas from the gas-liquid separation tank 7 so as to remove trace ammonia carried in the non-condensable gas.
Wherein, the utility model discloses in, be provided with the multilayer column plate in the washing device, can be according to the difference of handling load, select tower tray layer quantity. The non-condensable gas washed by the washing device is compressed by a compressor and then sent to a conversion unit to recover hydrogen and carbon monoxide.
In a preferred embodiment, the system further comprises a circulation pump 9, wherein the circulation pump 9 is arranged between the stripping cooler 5 and the gas-liquid separation tank 7, and is used for conveying the liquid phase separated in the gas-liquid separation tank 7 to the stripping cooler 5 to exchange heat with the stripping gas extracted from the top of the stripping tower 4.
In a preferred embodiment, the system further comprises a high-pressure flash gas line 10, and the high-pressure flash gas line 10 is connected with the stripping tower 4 and is used for conveying high-pressure flash gas to the stripping tower 4.
Wherein, the utility model discloses in, high pressure flash distillation gas comes from the gasification unit, gets into the strip tower from the bottom of strip tower, strips high temperature condensate, medium temperature condensate and low temperature condensate. The concentration of ammonia in the condensate liquid extracted from the bottom condensate liquid outlet of the stripping tower is below 200ppm, the temperature is 160-170 ℃, the pressure is 0.5-0.9MPa, and the condensate liquid can be returned to the gasification unit to be used as washing water after being pressurized by a pump.
In a preferred embodiment, the system further comprises an auxiliary steam line 11, said auxiliary steam line 11 being connected to said stripping column 4 for regulating the amount of steam entering said stripping column 4.
The utility model discloses in, transform condensate energy recuperation system's working process as follows:
the high-temperature condensate enters a second energy recovery module, is mixed with the medium-temperature condensate after heat recovery is completed in the second energy recovery module and then enters a third energy recovery module, and enters a stripping tower from the lower end of the stripping tower after pressure energy recovery is completed in the third energy recovery module;
the low-temperature condensate enters a first energy recovery module, and enters a stripping tower from the upper end of the stripping tower after pressure energy recovery is completed in the first energy recovery module;
high-pressure flash steam enters the stripping tower from the lower end of the stripping tower through a high-pressure flash steam pipeline, high-temperature condensate, medium-temperature condensate, low-temperature condensate and the high-pressure flash steam are stripped in the stripping tower, and the amount of steam entering the stripping tower is adjusted by an auxiliary steam pipeline in the stripping process;
pressurizing tower kettle materials extracted from a tower kettle of the stripping tower by a pump, conveying the tower kettle materials to a gasification unit, cooling a stripping gas extracted from the top of the stripping tower in two stages by a stripping cooler and a circulating water cooler, then feeding the cooled liquid phase in the gas-liquid separation tank back to the stripping cooler for cooling the stripping gas extracted from the top of the stripping tower, and then feeding the liquid phase into a carbon dioxide removal module to obtain dilute ammonia water which can be used as ammonia water or a liquid ammonia production raw material;
the noncondensable gas separated from the gas-liquid separation tank is washed by a washing device, compressed by a compressor and sent to a conversion unit to recover hydrogen and carbon monoxide.
The utility model provides a transform condensate energy recuperation system, but the temperature and the pressure of make full use of high temperature condensate and medium temperature condensate to and the pressure of low temperature condensate, reduce the quantity of the reboiling steam of low temperature condensate strip tower, improve the energy comprehensive utilization of whole technology and rate, be fit for the industrial production.
The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. In the technical idea scope of the present invention, it can be right to the technical solution of the present invention perform multiple simple modifications, including each technical feature combined in any other suitable manner, these simple modifications and combinations should be regarded as the disclosed content of the present invention, and all belong to the protection scope of the present invention.
Claims (7)
1. A shift condensate energy recovery system, characterized in that the system comprises a first energy recovery module (1), a second energy recovery module (2), a third energy recovery module (3) and a stripper (4); wherein the first energy recovery module (1) is connected to the stripping column (4), the second energy recovery module (2) is connected to the third energy recovery module (3), and the third energy recovery module (3) is connected to the stripping column (4);
wherein the first energy recovery module (1) is selected from a differential steam pressure power generation device and/or a pressure driven pump for recovering the pressure of the low-temperature condensate to generate electric energy and/or driving force;
wherein the second energy recovery module (2) is selected from a heat exchanger and/or a heat storage device and is used for recovering heat of high-temperature condensate;
wherein the third energy recovery module (3) is selected from a steam pressure difference power generation device and/or a pressure driven pump for recovering the pressure of the medium temperature condensate and the high temperature condensate from the second energy recovery module (2) to generate electric energy and/or driving force.
2. The system according to claim 1, characterized in that it further comprises a stripping cooler (5), a circulating water cooler (6) and a gas-liquid separation tank (7); wherein, stripping tower (4) in proper order with stripping cooler (5), circulating water cooler (6) and vapor-liquid separation jar (7) are connected, vapor-liquid separation jar (7) still with stripping cooler (5) are connected.
3. A system according to claim 2, characterized in that the top of the gas-liquid separation tank is provided with a scrubbing device (8), which scrubbing device (8) is used to scrub the non-condensable gasses from the gas-liquid separation tank (7) in order to remove traces of ammonia carried in the non-condensable gasses.
4. The system according to claim 2, characterized in that the system further comprises a circulation pump (9), the circulation pump (9) is arranged between the stripping cooler (5) and the gas-liquid separation tank (7) and is used for conveying the liquid phase separated from the gas-liquid separation tank (7) to the stripping cooler (5) to exchange heat with the stripping gas extracted from the top of the stripping tower (4).
5. The system according to claim 1, characterized in that the system further comprises a high-pressure flash gas line (10), the high-pressure flash gas line (10) being connected to the stripping column (4) for feeding high-pressure flash gas to the stripping column (4).
6. The system according to claim 1, characterized in that the system further comprises an auxiliary steam line (11), the auxiliary steam line (11) being connected to the stripping column (4) for adjusting the amount of steam entering the stripping column (4).
7. The system according to claim 1, characterized in that the stripping column (4) is a tray column; wherein the first energy recovery module (1) is connected with the top of the stripping tower (4) and is used for feeding the low-temperature condensate into a first tower plate of the stripping tower (4).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220456540.0U CN217535928U (en) | 2022-03-02 | 2022-03-02 | Conversion condensate energy recovery system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220456540.0U CN217535928U (en) | 2022-03-02 | 2022-03-02 | Conversion condensate energy recovery system |
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| Publication Number | Publication Date |
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| CN217535928U true CN217535928U (en) | 2022-10-04 |
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| CN202220456540.0U Active CN217535928U (en) | 2022-03-02 | 2022-03-02 | Conversion condensate energy recovery system |
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